Small cylindrical reformer

ABSTRACT

Disclosed herein is a small cylindrical reformer, which is suitable for use in the production of hydrogen from fossil fuels for a small fuel cell power plant. In the small cylindrical reformer according to this invention, a reforming reactor, a water gas shift reactor (high temperature or low temperature), a combustor, a heat exchanger, a steam generator, etc., may be integrated in a single container to form an optimal heat exchanging network, minimize heat loss and optimize heat exchange efficiency. Thereby, the reformer is designed to be easily processed and manufactured and to have a compact size, thus realizing high efficiency, light weight and ease of mass production.

CROSS REFERENCE OF RELATED APPLICATIONS

This application is a divisional of U.S. patent application Ser. No.11/296,061, filed Dec. 6, 2005, which claims priority to Korean PatentApplication Serial No. 10-2004-0102501, filed Dec. 7, 2004, both ofwhich are hereby incorporated by reference in their entireties.

BACKGROUND OF THE INVENTION

1. Field of the Invention

The present invention relates to a small cylindrical reformer, suitablefor use in the production of hydrogen from fossil fuels for a small fuelcell power plant, in which a reforming reactor, a water gas shiftreactor (high temperature or low temperature), a combustor, a heatexchanger, a Steam generator, etc., may be integrated in a singlecontainer to form an optimal heat exchanging network, minimize heat lossand optimize heat exchange efficiency, whereby the reformer is designedto be easily processed and manufactured and to have a compact size,resulting in high efficiency, light weight and ease of mass production.

2. Description of the Related Art

Presently, as the type of fuel to be consumed is gradually moving towardclean fuel having a high hydrogen/carbon-atom ratio and a low pollutionlevel, an industrial society based on hydrogen as a harmless clean fuelis expected to arise quickly. In industrial fields, hydrogen has alreadybeen applied to ammonia synthesis, methanol synthesis, petroleumrefining (dehydrogenation, hydrogenation, etc.), general and finechemical industries, electronic and semiconductor industries, food andmetal processing industries, etc. Further, in the energy fields,hydrogen is used as the fuel of fuel cells for home or power plants andof power supply sources for fuel cell automobiles, being able to solveat one time problems, related to a propellant, electric power supply andenergy efficiency of a space shuttle, in which an internal combustionengine is not used, and to environmental pollution, at one time.

Presently available methods of preparing hydrogen include, for example,steam reforming, partial oxidation or autothermal reforming of fossilfuel (coal, petroleum, natural gas, propane, butane), and waterelectrolysis. Although hydrogen may be obtained from a by-product gas ofa petroleum refining process, the steam reforming method is regarded asan economical application technique which is most widely usedcommercially.

In the case where the steam reforming method is applied to producehydrogen on a large scale, a reforming reactor may be operated at a highpressure (15-25 bar) and high temperature (850° C. or higher). Thereby,hydrogen may be desirably produced, but the total efficiency thereof islow. In addition, when producing hydrogen on a small scale, theinstallation cost may be drastically increased. In addition, theapparatus may be enlarged for stable operation, and each process may beseparately conducted, thus it is difficult to increase heat efficiencydue to the limitation in combining heat.

Hence, in order to solve the above drawbacks of reformers for home orcommercial small fuel cell systems, attempts have been made to combineeach process, develop a catalyst suitable for a small fuel cell system,optimize the reformer using a heat flow analysis, simplify the structureof the reformer to increase proccessability and productivity, andintegrate constituents of the reformer to decrease the size thereof, soas to reduce initial start-up time and heat loss and increase heatefficiency.

In this regard, U.S. Pat. No. 5,932,181 discloses a hydrogen generatorusing a cylindrical combustion catalyst, which comprises adesulfurization reactor, a reforming reactor, a water gas shift reactor,a pressure swing absorption unit, etc. This patent is advantageousbecause the number of parts of equipment is decreased so that the spacenecessary to set it up may be reduced to miniaturize the generator, andthe manufacturing cost is drastically decreased, and also efficiency andstart-up time may be improved by heat exchanging the desulfurizationreactor. In the above generator, heat generated from the desulfurizationreactor, the reforming reactor, the steam generator and the combustormay be combined together, however heat generated from the water gasshift reactor and the subsequent parts cannot be combined, thusdecreasing the total heat efficiency and increasing the size of thedevice.

In addition, U.S. Pat. No. 6,117,578 discloses a reformer for fuel cellpower plants using two heat supply sources of a combustion catalyst or aburner, in which a combustion catalyst and a reforming catalyst areapplied on the wall in the reformer to maximize catalyst efficiency, andthus, the reformer may be operated even at a low temperature. Thereby,reaction operation conditions become mild. However, high heat efficiencyis difficult to obtain, due to the lack of combination of postprocesses.

Korean Patent Laid-open Publication No. 2002-82061 discloses a compactsteam reformer using a cylindrical metal fiber burner, in which areactor, a heat exchanger and a steam generator may be integrated,realizing the compact steam reformer. Further, as the heat supply sourcenecessary for reforming, the cylindrical metal fiber burner is used foruniform heating, whereby the temperature gradient of the catalyst layerin the reforming reactor may be reduced to maximize reformingefficiency. Also, since steam is generated using a combustion exhaustgas, energy efficiency increases, and an additional steam generator isnot needed, resulting in a highly simplified system and decreased deviceand operation costs. However, in the above reformer, a heat streaming isnot optimized, and the exhaust gas stream should be accuratelycontrolled during operation. Further, excessive fuel is consumed, andheat generated from the water gas shift reactor and the preferentialoxidation reactor is not recovered, decreasing the heat efficiency.Furthermore, heat exchange between the exhaust gas and the steam resultsin an undesirably enlarged reformer.

Recently, U.S. Pat. No. 6,481,207 discloses a cylinder type reformer foruse in maximizing heat efficiency, in which a burner is provided at thecentral upper portion of the reformer, and a plurality of cylinders aresequentially radially disposed from the highest temperature region tothe lowest temperature region to maximally suppress heat loss. Inaddition, the cylinders are attempted to be integrated while increasingheat efficiency by conducting heat exchange therebetween. The reformeris designed in such a way that the reactor is axially positioned so asto enable the cylinder type reforming reactor to resist thermaldeformation. In the above reformer, a preheating layer and a heatrecovery layer are provided for effective heat exchange. However, thereis no means for preheating air, and also many spaces for liquidstagnation are present in the structure, and hence, problems may occurwhen water is not completely evaporated or the product is condensed.Further, the above reformer is not easy to manufacture due to itscomplicated structure.

SUMMARY OF THE INVENTION

Accordingly, the present invention has been made keeping in mind theabove problems of the small reformers occurring in the prior art, and anobject of the present invention is to provide a small cylindricalreformer, which comprises a reforming reactor, a water gas shift reactor(high temperature or low temperature), a combustor, a heat exchanger, asteam generator, etc., integrated in a single container to form anoptimal heat exchanging network capable of exhibiting excellentperformance.

Another object of the present invention is to provide a smallcylindrical reformer, which is structured to minimize heat loss andexhibit optimal heat exchange efficiency, whereby the reformer has highheat efficiency despite having a compact size, is easily processed andmanufactured, and simplifies a fluid stream flowing therein to minimizestagnation spaces, resulting in high efficiency, light weight, and easeof mass production.

In order to accomplish the above objects, the present invention providesa small cylindrical reformer, comprising a combustion reaction unit,which includes a combustion part to burn air and fuel supplied from anair/fuel inlet, a combustion gas distributor to distribute thecombustion gas burned in the combustion part, and a first combustion gaspassage and a second combustion gas passage to guide the distributedcombustion gas into an outlet to be discharged; and a fuel-convertingcatalytic reaction unit, which includes two reforming reaction partseach having a reforming catalyst to reform feed and water supplied froma feed/water inlet, to prepare a reforming reaction reformate, and awater gas shift reaction part formed between the two reforming reactionparts to decrease the concentration of carbon monoxide in the reformingreaction reformate, to prepare a water gas shift reformate, in which thecombustion reaction unit and the fuel-converting catalytic reaction unitare integrally structured by six cylindrical pipes to realize optimalheat exchange efficiency.

BRIEF DESCRIPTION OF THE DRAWINGS

The above and other objects, features and advantages of the presentinvention will be more clearly understood from the following detaileddescription taken in conjunction with the accompanying drawings, inwhich:

FIG. 1 is a longitudinal sectional view showing the internal structureof a small cylindrical reformer, according to a first embodiment of thepresent invention;

FIG. 2 is a longitudinal sectional view showing the internal structureof a small cylindrical reformer, according to a second embodiment of thepresent invention;

FIG. 3 is a longitudinal sectional view showing the internal structureof a small cylindrical reformer, according to a third embodiment of thepresent invention;

FIG. 4A is a transverse sectional view showing the small cylindricalreformer according to the first embodiment of the present invention, andFIG. 4B is a transverse sectional view showing the small cylindricalreformer according to the second embodiment of the present invention;and

FIG. 5 is a schematic view showing the small cylindrical reformerfurther comprising a heat exchanger, according to the present invention.

DESCRIPTION OF THE PREFERRED EMBODIMENTS

Hereinafter, a detailed description will be given of the presentinvention, with reference to the appended drawings.

FIG. 1 is a longitudinal sectional view showing the internal structureof a small cylindrical reformer, according to a first embodiment of thepresent invention. FIGS. 2 and 3 are longitudinal sectional viewsshowing small cylindrical reformers, according to a second embodimentand a third embodiment, respectively, of the present invention. FIGS. 4Aand 4B are transverse sectional views showing the small cylindricalreformers, according to the first embodiment and the second embodiment,respectively, of the present invention. FIG. 5 is a schematic viewshowing a small cylindrical reformer further comprising a small heatexchanger, according to the present invention.

Referring to FIG. 1, the small cylindrical reformer according to thefirst embodiment of the present invention is specifically explained. Thesmall cylindrical reformer comprises two units, that is, a combustionreaction unit and a fuel-converting catalytic reaction unit. Thecombustion reaction unit includes a combustion part to burn air and fuelsupplied from an air/fuel inlet 1, a combustion gas distributor 15 todistribute the combustion gas burned in the combustion part, and firstand second combustion gas passages 20 and 21 to guide the distributedcombustion gas into an outlet 2 to be discharged. In addition, thefuel-converting catalytic reaction unit is composed of two reformingreaction parts, each including a reforming catalyst to reform feed andwater supplied from a feed/water inlet 3, and a water gas shift reactionpart, formed between the two reforming reaction parts to conduct a watergas shift reaction so as to decrease the concentration of carbonmonoxide in a reforming reaction reformate obtained through thereforming reaction.

Moreover, the combustion reaction unit and the fuel-converting catalyticreaction unit are integrally structured by six cylindrical pipes torealize optimal heat exchange efficiency. Thereby, a network for optimalheat exchange efficiency may be achieved. Further, the fuel-convertingcatalytic reaction unit may further comprise a preferential oxidationreactor at the outside thereof to decrease the content of carbonmonoxide discharged from the water gas shift reaction part to apredetermined level or lower.

In the small fuel reformer thus structured, the combustion part includesa first air/fuel preheating passage 10, a combustion chamber 14, and anair preheating tube 13 provided around the first air/fuel preheatingpassage 10 to preheat air. The first air/fuel preheating passage 10 is aspace where the air and fuel supplied from the air/fuel inlet 1 arepreheated before being introduced into the combustion chamber 14. Assuch, the preheating process minimizes the heat requirement of thecombustion chamber 14. Such a preheating process is conducted using theair preheating tube 13 provided around the first air/fuel preheatingpassage 10, in which heat stored in the air preheating tube 13 isobtained via a first combustion gas passage 20 to guide the combustiongas burned in the combustion chamber 14 to be externally discharged.

The air and fuel passed through the first air/fuel preheating passage 10are supplied into the combustion chamber 14 to burn them. The combustiongas thus obtained is uniformly distributed into the first combustion gaspassage 20 and the second combustion gas passage 21 using the combustiongas distributor 15 provided at the upper portion of the combustionchamber 14. The combustion gas distributor 15 is sheet-shaped so as torealize appropriate distribution into the first combustion gas passage20 and the second combustion gas passage 21.

The distributed combustion gas is guided into the exhaust gas outlet 2through the first combustion gas passage 20 and the second combustiongas passage 21, and is then discharged. The first combustion gas passage20 and the second combustion gas passage 21 function to transfer heatinto the two reforming reaction parts formed therebetween. Inparticular, the first combustion gas passage 20 is used to transfer heatinto the air preheating tube 13, in addition to transferring heat intothe reforming reaction part, to maximally utilize heat of the dischargedcombustion gas. Further, the second combustion gas passage 21, throughwhich the combustion gas is passed, directly contacts a fourth pipe 18forming the reformer. Hence, Al₂O₃ may be deposited on the internalsurface of the fourth pipe 18, using Al alloy or clad metal material, orceramic material may be attached thereto for heat insulation at a hightemperature region. Thereby, heat loss may be minimized or oxidationcorrosion due to the combustion gas may be prevented.

The first air/fuel preheating passage 10 and the first and secondcombustion gas passages 20 and 21 have variable spaces between them forappropriate heat exchange. As such, a heat transfer increasing material,formed of a metal in such a way that pressure drops only slightly, maybe inserted to increase heat exchange efficiency. In addition, a supportmay be inserted to maintain the above space at a predetermined level andincrease heat transfer. The metal support may be formed of sphericalmetal balls, metal mesh having a predetermined lattice size, or wovenmetal to prevent lop-sided channeling of a gas stream so as to induce asmooth stream. As such, a metal material, which is not deformed at ahigh temperature, does not heat expand, and does not corrode due tosurface oxidation, may be selected, and preferably, a product made ofstainless steel may be used.

The fuel-converting catalytic reaction unit of the reformer consists ofthe two reforming reaction parts, the water gas shift reaction partformed between the two reforming reaction parts, and the preferentialoxidation reactor. Of these parts, the reforming reaction part is firstexplained. Namely, the two reforming reaction parts each include afeed/water preheater 32 to preheat feed and water supplied from afeed/water inlet 3, a feed/water superheater 33 to superheat thepreheated feed and water, and a reforming reactor 36 to conduct thereforming reaction of the superheated feed and water.

Specifically, the feed and water supplied from the feed/water inlet 3are introduced into the reforming pipes through feed/water passages 30and 31, so that they are preheated and superheated using the feed/waterpreheaters 32 and the feed/water superheaters 33 while moving upwards.The preheating and superheating processes are conducted by heat exchangewith the first and second combustion gas passages 20 and 21 formedaround the reforming reaction part, and further by heat exchange withthe water gas shift reaction part formed between the two reformingreaction parts. The feed/water preheater 32 and the feed/watersuperheater 33 are filled with ceramic balls having a diameter such thatpressure drops only slightly. The ceramic filler may be in the form ofspheres, flakes, or cylinders. Preferably, for a smooth fluid stream,the spherical ceramic filler may be used, the diameter of which has asize ranging from 1/10 to ⅓ of the filling space, without exceeding anerror range of 10%. Moreover, it is preferable that a filler productcomposed only of a main component, such as alumina, silica or magnesia,or of a mixture comprising the main component, selected from amongalumina, silica, magnesia and combinations thereof, and an auxiliarycomponent, be used, in consideration of heat exchange efficiency. Thefeed/water preheater 32 and the feed/water superheater 33 perform doubleheat exchange with the first and second combustion gas passages 20 and21 and with the water gas shift reaction part, to realize optimal heattransfer efficiency.

The feed passed through the superheaters 33 is supplied into thereforming reactors 36 and contacts the steam reforming catalysts loadedtherein to conduct a reforming reaction, and is thus converted into areforming reaction reformate comprising hydrogen, carbon monoxide,carbon dioxide and water. The reforming catalyst causing the abovereaction includes, for example, an Ni-based steam reforming catalyst, oran Ni-based steam reforming catalyst containing at least 0.01 wt %precious metal such as Pt or Ru. The diameter of the reforming catalystpreferably has a size ranging from 1/10 to ⅓ of the space defining thereforming reaction part, in consideration of pressure drop andreactivity in the pipes.

The reforming reaction reformate formed through the two reformingreaction parts is supplied into the water gas shift reaction partbetween the two pipes, in which the water gas shift reaction partincludes a first reforming reaction reformate passage 37 and a secondreforming reaction reformate passage 38 to conduct efficient heatexchange so that the temperature of the reforming reaction reformatepassed through the reforming reaction parts decreases to a predeterminedlevel, and a water gas shift reactor 39 to decrease the concentration ofcarbon monoxide in the above reforming reaction reformate to apredetermined level or lower.

The first reforming reaction reformate passage 37 and the secondreforming reaction reformate passage 38, acting similarly to thepreheaters and superheaters formed in the two reforming reaction parts,are used to decrease the temperature of the reforming reactionreformate, produced through the reforming reaction parts, viaappropriate heat exchange, and therefore, are filled with ceramic ballshaving a diameter such that pressure drops only slightly as in thefeed/water preheater 32 and the feed/water superheater 33. The ceramicfiller may be in the form of spheres, flakes, or cylinders. Inparticular, for a smooth fluid stream, the spherical ceramic filler maybe preferably used, the diameter of which has a size ranging from 1/10to ⅓ of the filling space, without exceeding an error range of 10%. Inconsideration of the heat exchange efficiency, as the filler, a productcomposed only of a main component such as alumina, silica, or magnesia,or of a mixture comprising a main component selected from among alumina,silica, magnesia and combinations thereof and an auxiliary component maybe preferably used. The use of such an internal material permits theheat transfer efficiency to increase, heat to be stored or thetemperature to be uniformly maintained in the predetermined range.

The reforming reaction reformate resulting from the reforming reaction,which is decreased in the temperature by passing through the firstreforming reaction reformate passage 37 and the second reformingreaction reformate passage 38, is supplied into the water gas shiftreactor 39. Thereby, the above reformate is subjected to a water gasshift reaction while contacting the water gas shift catalyst, so thatthe concentration of carbon monoxide in the reformate is decreased from7-15% to 0.3-1.0%. As such, the water gas shift catalyst causing theabove reaction includes, for example, an Fe—Cr-based high temperatureshift catalyst, a Cu—Zn-based low temperature shift catalyst, or a watergas shift catalyst containing at least 0.01 wt % precious metal such asPt or Pd. The diameter of the catalyst has a size ranging from 1/10 to ⅓of the space defining the water gas shift reaction part, inconsideration of pressure drop and reactivity in the pipes.

The water gas shift reformate produced through the water gas shiftreaction part is combined into one stream via first and second water gasshift reformate passages 40 and 41, externally discharged, passedthrough a water gas shift reformate/air passage 42 to be mixed with airrequired for a preferential oxidation so as to obtain a temperaturesuitable for preferential oxidation, and then introduced into thepreferential oxidation reactor 43. While the supplied water gas shiftreformate contacts the preferential oxidation catalyst loaded in thepreferential oxidation reactor 43, it undergoes preferential oxidationso that the concentration of carbon monoxide in the reformate dischargedfrom the water gas shift reactor is decreased from 0.3-1.0% to 10 ppm orless. At this time, the preferential oxidation catalyst contains atleast 0.05 wt % of one or two selected from among Pt, Ru, and Au, thediameter of which has a size ranging from 1/10 to ⅓ of the spacedefining the water gas shift reaction part, in consideration of pressuredrop and reactivity in the pipes. The water gas shift reformate thusobtained is discharged through the outlet 5.

In the present invention, the reformer may further include a heatexchanger at the outside thereof to conduct heat exchange using waterwhich is supplied, thus recovering heat from a finally dischargedexhaust gas 2. Thereby, total heat efficiency can increase. That is, sixcylindrical pipes are integrated, and therefore, a network for optimalheat exchange may be realized. Such a structure is advantageous becausestagnation spaces in the heat stream of the combustion part and thereforming part are not formed, thus increasing the efficiency.

Moreover, the operation of the reformer of the present invention isexplained with reference to the drawings.

FIG. 1 shows the internal structure of the small cylindrical reformer,according to the first embodiment of the present invention. The smallcylindrical reformer of the present invention performs two processes,that is, a combustion process and a reforming process. For thecombustion process, air and fuel supplied from the inlet 1 arepreheated, burned in the combustion chamber 14 using a burner 11 togenerate heat, and then uniformly distributed into the first and secondcombustion gas passages 20 and 21 through the combustion gas distributor15. While passing through the above passages 20 and 21, the combustiongas transfers heat into the reforming reactor 36, the feed/watersuperheaters 33, water preheaters 32 and the first air/fuel preheatingpassage 10, and is then discharged through the exhaust gas outlet 2.

For the reforming process, feed and water supplied from the inlet 3 areintroduced into the feed/water preheaters 32 through the first andsecond exhaust gas passages 30 and 31 to recover heat from the exhaustgas and from the water gas shift reactor, introduced into the feed/watersuperheaters 33 to recover heat from the exhaust gas and from thereforming reaction reformate obtained through the reforming reaction,and then supplied into the reforming reactors 36 to undergo thereforming reaction. Subsequently, the reforming reaction reformate thusobtained is cooled to a suitable temperature while passing through thefirst and second reforming reaction reformate passages 37 and 38, andsupplied into the water gas shift reactor 39 to undergo the water gasshift reaction so as to obtain a water gas shift reformate, which isthen passed through the first and second water gas shift reformatepassages 40 and 41 to be discharged, passed through the water gas shiftreformate/air passage 42 to be mixed with air required for apreferential oxidation, supplied into the preferential oxidation reactor43 to remove residual carbon monoxide, and then finally dischargedthrough the water gas shift reformate outlet 5.

The above processes are described in detail below. As the fuel loadedinto the air/fuel inlet 1, fossil fuel for reforming is initially usedand then mixed with air. During operation, unused offgas in a fuel cellstack is mainly used, and the fossil fuel is auxiliarily used to controlheat.

The preheated air and fuel are burned using the burner 11 able to safelyburn both fossil fuel and offgas of the fuel cell stack to producecarbon dioxide and water, first transfer radiant heat to the peripheralreforming reactors, and are then appropriately distributed through thecombustion gas distributor 15. As is apparent from the transversesectional view of the small cylindrical reformer of the presentinvention shown in FIG. 4A, the main reactor is composed of sixcylindrical pipes, including a first pipe 12 defining a combustionchamber, a fourth pipe 18 surrounding the whole reactor, and a secondpipe 16, a fifth pipe 34, a sixth pipe 35 and a third pipe 17 radiallypositioned between the first pipe 12 and the fourth pipe 18. The firstcombustion gas passage 20 is defined into a space between the first pipe12 and the second pipe 16, and the second combustion gas passage 21 intoa space between the third pipe 17 and the fourth pipe 18. Hence, afterthe combustion gas passing through the above passages 20 and 21transfers heat to ambient air, the reforming reactors 36, the feed/watersuperheaters 33, and the feed/water preheaters 32, it is dischargedthrough the exhaust gas outlet. As can be seen in FIG. 1, the combustiongas passed through first and second combustion gas passages 20 and 21are combined into one stream through an exhaust gas connection passage22, and are then discharged via an exhaust gas passage 23.

In addition, the feed and water supplied from the inlet 3 are dividedbetween the two feed/water preheaters 32 through the first and secondfeed/water passages 30 and 31, some of which is supplied into thepreheater positioned between the second pipe 16 and the fifth pipe 34,the rest of which is supplied into the preheater positioned between thethird pipe 17 and the sixth pipe 35. Therefore, heat may be recoveredfrom the combustion gas and water gas shift reactor 39.

The preheated feed is supplied into the feed/water superheaters 33 torecover heat from the combustion gas and from the reforming reactionreformate, and the superheated feed is supplied into the reformingreactors 36 to undergo the reforming reaction while contacting theloaded steam reforming catalyst and is thus converted into a reformingreaction reformate comprising hydrogen, carbon monoxide, carbon dioxide,unreacted feed, and excess water. The reforming reaction reformatetransfers heat to the reforming reactors 36 and the feed/watersuperheaters 33 while passing through the first reforming reactionreformate passage 37 and the second reforming reaction reformate passage38, whereby the temperature thereof is decreased.

The reforming reaction reformate appropriately cooled to the temperaturerequired for the water gas shift reaction is supplied into the water gasshift reactor 39 to undergo the water gas shift reaction whilecontacting the loaded water gas shift catalyst. Thereby, theconcentration of carbon monoxide in the above reformate is decreasedfrom 7-15% to 0.3-1.0%. The water gas shift reformate produced throughthe water gas shift reactor 39 is passed through the first and secondwater gas shift reformate passages 40 and 41 to be combined into onestream, which is then externally discharged. The discharged reformate ispassed through the water gas shift reformate/air passage 42 to be mixedwith air 4 required for preferential oxidation so as to have thetemperature suitable for preferential oxidation, and is then suppliedinto the preferential oxidation reactor 43.

Subsequently, the supplied water gas shift reformate is subjected topreferential oxidation while contacting the preferential oxidationcatalyst loaded in the preferential oxidation reactor 43 to decrease theconcentration of carbon monoxide in the shift reformate obtained usingthe water gas shift reactor from 0.3-1.0% to 10 ppm or lower, and isthen discharged through the water gas shift reformate outlet 5.

FIG. 2 is a longitudinal sectional view showing the internal structureof a small cylindrical reformer, according to the second embodiment ofthe present invention, in which a preferential oxidation reactor 43 ispositioned differently from that shown in FIG. 1 to increase space usageand heat exchange efficiency.

That is, the preferential oxidation reactor 43, which is formed at theoutside of the reformer as shown in FIG. 1, may be provided betweenfirst air/fuel preheating passages 10 in FIG. 2. When the preferentialoxidation reactor 43 is formed between the first air/fuel preheatingpassages 10, heat exchange between the preferential oxidation reactor 43and the first air preheating passages 10 is accelerated, thus increasingthe total heat efficiency of the system.

FIG. 4B is a transverse sectional view showing the small cylindricalreformer, according to the second embodiment. As shown in this drawing,while the introduced air and fuel are supplied into preheating regionsamong a first pipe 12, a seventh pipe 44 and an eighth pipe 45 and arethen passed through the air/fuel preheating passages 10, heat may berecovered from the preferential oxidation reactor 43 and from theexhaust gas. The above passages may be controlled in the spaces thereoffor appropriate heat exchange, into which any metal material able toincrease heat exchange efficiency while not decreasing the pressure maybe inserted.

That is, a water gas shift reformate produced using a water gas shiftreactor 39 is combined into one stream through the passages 40 and 41,and is then supplied into the preferential oxidation reactor 43. Thesupplied water gas shift reformate is subjected to preferentialoxidation in the presence of a preferential oxidation catalyst loaded inthe preferential oxidation reactor 43 to decrease the concentration ofcarbon monoxide in the shift reformate from 0.3-1.0% to 10 ppm or lower,and is thereafter discharged through a reformate outlet 5.

FIG. 3 is a longitudinal sectional view showing the internal structureof a small cylindrical reformer, according to the third embodiment ofthe present invention. This small cylindrical reformer comprises acombustion reaction unit including a combustion part to burn air andfuel supplied from an air/fuel inlet 1, a combustion gas distributor 15to distribute the combustion gas burned in the combustion part, andfirst and second combustion gas passages 20 and 21 to guide thedistributed combustion gas into an outlet 2 to be discharged, and afuel-converting catalytic reaction unit including two reforming reactionparts each having a reforming catalyst to reform feed and water suppliedfrom a feed/water inlet 3, and a water gas shift reaction part formedbetween the two reforming reaction parts to conduct a water gas shiftreaction able to decrease the concentration of carbon monoxide in areforming reaction reformate resulting from the reforming reaction, inwhich the combustion reaction unit and the fuel-converting catalyticreaction unit are integrally structured by six cylindrical pipes torealize optimal heat exchange efficiency.

At the lower portion of the above reformer, a route for supplying thewater gas shift reformate passed through the water gas shift reactionpart into the preferential oxidation reactor, and a route for supplyingfeed and water into the reforming reaction parts from the feed/waterinlet 3 are designed to overlap each other so as to increase the heattransfer efficiency. Further, the preferential oxidation reactor 43,which is used to decrease the concentration of carbon monoxide in thewater gas shift reformate passed through the water gas shift reactionpart to a predetermined level or lower, is positioned at the lowerportion of the above route, so as to increase the heat transferefficiency with a second air/fuel preheating passage 52 communicatingwith the air/fuel inlet 1.

That is, in the reformer according to the third embodiment of thepresent invention, an increase in heat transfer efficiency is expectedby positioning the preferential oxidation reactor 43 at the lowerportion of the reformer. As such, with the aim of obtaining high heattransfer efficiency, a plurality of air/fuel distributors 51 should beprovided between the preferential oxidation reactor 43 and the secondair/fuel preheating passage 52 for effective heat distribution.

In addition, the preferential oxidation reactor 43 formed at the lowerportion of the reformer may be assembled along with the second air/fuelpreheating passage 52, and thus, the assembly of the small fuel reformermay be more easily conducted.

FIG. 5 is a schematic view showing a reformer further comprising a heatexchanger, according to the present invention. That is, a small heatexchanger 53 may be additionally provided to the reformer of FIG. 1, toachieve heat exchange between the discharged exhaust gas 2 and water 54to be supplied, thus increasing the total heat efficiency. In this way,a small heat exchanger 53 may be also additionally provided in thereformer of FIG. 2 or 3, to achieve heat exchange between the dischargedexhaust gas 2 and water 54 to be supplied, thus increasing the totalheat efficiency.

In the present invention, constituents, such as a catalyst reactor, acombustor, a heat exchanger, etc., were integrated in a single containerfor an optimal heat exchanging network, thus manufacturing a smallcylindrical reformer. When such a reformer was operated, a methaneconversion rate was 94% or more, a CO content after the water gas shiftreaction was 0.7% or less, and a CO content after the PROX was 10 ppm orless. As well, high heat transfer efficiency was realized.

Further, in the heat transfer efficiency, optimal heat efficiency may beobtained via heat exchange between two or more fluids while conductingcombustion reactions in the presence of a catalyst suitable for eachreaction. These constituents may be integrated in a single reactor sothat the resultant apparatus is structured to have a compact size whileminimizing heat loss. In addition, six pipes constituting the apparatusmay be designed to be integrated, and thus, easily processed andmanufactured.

As described hereinbefore, the present invention provides a smallcylindrical reformer. According to the small cylindrical reformer forfuel cell power plants of the present invention, a reforming reactor, awater gas shift reactor (high temperature or low temperature), acombustor, a heat exchanger, a steam generator, etc., may be integratedin a single container, so that an optimal heat exchanging network ableto exhibit maximal performance of each constituent is manufactured.Thereby, the resultant reformer is advantageous because it is structuredto exhibit minimal heat loss and optimal heat exchange efficiency. Inthis way, the reformer is designed to have a compact size and be easilyprocessed and manufactured even while having high heat efficiency. Inaddition, a fluid stream is simplified to minimize stagnation spaces. Inconsideration of expansion and constriction of the material used due tofrequent starting and stoppage, high efficiency, light weight, and massproduction are easily realized and durability is also exhibited. Hence,when the reformer is applied to a fuel cell power system, the totalpower efficiency can be increased. Moreover, since the reformer islightweight, it can be promptly operated according to initial start-uptime or operation capacity change. Also, the reformer can be favorablycommercialized through designs able to easily realize mass productionand durability.

Although the preferred embodiments of the present invention have beendisclosed for illustrative purposes, those skilled in the art willappreciate that various modifications, additions and substitutions arepossible, without departing from the scope and spirit of the inventionas disclosed in the accompanying claims.

1-20. (canceled)
 21. A small cylindrical reformer, comprising: acombustion unit, which includes: a combustion part to burn air and fuelsupplied from an air fuel inlet, a combustion gas distributor todistribute the combustion gas burned in the combustion part, and a firstcombustion gas passage and a second combustion gas passage to guide thedistributed combustion gas into an outlet to be discharged; and afuel-converting catalytic reaction unit, which includes: two reformingreaction parts preparing a reforming reaction reformate, each having areforming catalyst to reform feed and water supplied from a fee/waterinlet, and a water gas shift reaction part preparing a water gas shiftreformate, between the two reforming reaction parts to decrease aconcentration of carbon monoxide in the reforming reacting reformate,wherein the combustion reaction unit and the fuel-converting catalyticreaction unit are structured as six cylindrical pipes to realize optimalheat exchange efficiency, and preferential oxidation reactor is providedbetween first air fuel preheating passages in the combustion part todecrease the concentration of carbon monoxide in the water gas shiftreformate to a predetermined level or lower.
 22. The reformer as setforth in claim 21, wherein the preferential oxidation reactor includes apredetermined number of pipes to increase heat transfer efficiency. 23.A small cylindrical reformer, comprising: a combustion reaction unit,which includes: a combustion part burning air and fuel supplied from anair/fuel inlet, a combustion gas distributor distributing the combustiongas generated in the combustion part, and a first combustion gas passageand a second combustion gas passage to guide the distributed combustiongas into an outlet to be discharged; and a fuel-converting catalyticreaction unit including: two reforming reaction parts preparing areforming reaction reformats, each having a reforming catalyst to reformfeed and water supplied from a feed/water inlet; and a water gas shiftreaction part preparing a water gas shift reformate, between the tworeforming reaction parts to decrease a concentration of carbon monoxidein the reforming reaction reformate, wherein the combustion reactionunit and the fuel-converting catalytic reaction unit are structured assix cylindrical pipes to realize optimal heat exchange efficiently, aroute supplying the water gas shift reformate and a preferentialoxidation reactor and a route supplying feed and water into thereforming reaction parts from the feed/water inlet overlap each other ata lower portion of the reformer so as to increase heat transferefficiency, and the preferential oxidation reactor provided at the lowerportion of the reformer to decrease the concentration of carbon monoxidein the water gas shift reformate to a predetermined level or lower andincrease heat transfer efficiency with an air/fuel preheating passagecommunicating with the air/fuel inlet.
 24. The reformer as set forth inclaim 23, wherein the preferential oxidation reactor includes asheet-shaped air/fuel distributor for heat exchange with air and fuelsupplied from the air/fuel inlet.
 25. The reformer as set forth in claim23, wherein the preferential oxidation reactor and the air/fuelpreheating passage provided at the lower portion of the reformer areremovably attached to the small reformer.